Fluidized solids technique



uly 5, 19 0 A. R. HUNTLEY ETAL 2,944,009

FLUIDIZED SOLIDS TECHNIQUE 2 Sheets-Sheet 1 Filed Sept. 3, 1957 FIGURE 2 Allen R. Huntley Francis R. Russell Inventors By Attorney July 5, 1960 A. R HUNTLEY ET AL 2,944,009

FLUIDIZED SOLIDS TECHNIQUE Filed Sept. 3, 1957 2 Sheets-Sheet 2 Inventors sees es @090 ease sees eeeoeeee eeoeee eaeoeeeoe eeeeeeeeeeeeeeee FIGURE 4 tats operations involving'the contacting .oftwo or more phases, such as liquid-liquidcontacting,;e.g.,-during a solvent extraction-tot a' material from a-liquidbya liquidsolvent.

The present invention has particular application-in the gasiform-solids contacting in systems in which gasiform materials,1such'as hydrocarbons; are contacted with a dry, powdered solidfreactant, catalyst or heattransfer agent) in the'formof' a dense, fluidized, liquid-simulating bed or mass. Prior to'this invention, the fluidized solids technique was well known and practiced commercially in this country and abroad fon alarge: scale. The fluidized solids technique has been applied ,very; succ.essfully,;jfor ,example, to the catalytic cracking of gas oil. ln hydroforminghowever, a process wherein the naphtha vapors to be hydroformed are'caused to" flow upwardly through a dense'fluidized bed of catalyst at pressures considerably above atmospheric pressure, the gas=solids contacting has assess tial degree of catalyst contact.

specific object of the invention is to improve gasiform and solids contacting in fluidized'catalyst beds, particularly of naphtha with'finely divided *hydroformin'g catalyst particles-in areactor maintained at cpnventional hydroforming reaction conditions wherein the superficial upwaid'velocityof the gasiform material effecting fluidization is relatively low, by disposing in said bed spaced, perforate baflie means-affording lowresistanceto gas flow therethrough-and of such form and-construction as to minimize lateral gas flow.

Theseandother objectswillappear more clearly from I the detailed specification'and' claims which follow.

not 'been =satisfactory":due' largely toithe fact that the relativelylow vapor velocity-upwardly through thebed of catalyst permitst the vformation of relatively large gas bubbles causing channeling and bypassing without effective contact of' portions of the, upwardly flowing vapors with the catalyst particlesand other unsatisfactory operating conditions; It has. been proposed to, employ spaced perforated baffies disposed within the bed of solids in an attempt'to improvecgas-solids contacting mainly by the prevention of vapor channeling and large. gas bubble formation. Thus 'flat: perforated bafiies of high and-low pressure drop haverbeen disposed in reactors containing dense, fluidized beds :of finely divided solids. However, these have'not corrected-the foregoing defects. Such gas channelinghas been observed visuallyin laboratoryrtests in glass'vessels provided with conventional horizontal tubes or plates, using'air and water. These horizontal surfaces tended to agglomerate small bubbles into large ones, which flowed horizontally beneath the baflies and rose rapidly, forming channels along the wall. This channeling was alsoseen with air and fluidized solids. The problem is much worse .when the baflie is tilted slightly from a true horizontal position, a condition which. is likely toaoccur in large vessels. The net effect of conventional baflies in 1a fluidized bed can therefore be harmful. Furthermore, ithasbeen also proposed to, employ .in place of .flat.perforated baffles various other types of baifles .of different geometric configurations, such as baffles which: are wave-like, undulating, corrugated and 'thedike in shape. .However, experiments have shown -that1such1bafiies: are not, satisfactory with respect toethe :above 'interrphase contacting. 1 L The main object ofthe present invention is to provid improved perforate baifle means of such form and .construction and so disposed in a treating'zone as to cause .maximum. contacting between gasiform materials. and

liquids or finely divided solid particles 5? it ,Anotherobject of the invention is to improve contact- ;ingiefliciency for vaporphase reactions carried outin the presence of a fluidized bed of solids 'by providing withsaid=hed a;p1urality ofsperforate baffling means which i Briefly, the present invention in a specific modification involves' improvements in the operation of a-process eni- V ploying fluidized solids effected by disposingfwithinthe dense fluidized bed one or a plurality of'p'er for ated baifles,

the perforations-of which are sufliciently large to permit gas flow therethrough at a low pressure'decrease across the 'bafiie or bafiies, say one not exceeding about one-half p.s.i., the said baifles being of a configuration or shape as. tofonn numerous pockets inor beneath the baifleto trap the rising gasifcrm material so that its flow horizontally is restricted and is forced 'up through that pocket of the baiile which it first-entered; Channeling of large gas bubbles up one side of the bed,; which occurs "With conventional b'a'fijes, is thus prevented. In addition, any

large gas bubbles or any--massive solid streams'vvill be broken up, redispersed, and-redistributed by such bafiies. This invention includes; severaldifferent baflie designs which will operate in the manner above described-The preferred design is a perforated wave-like or corrugated plate carrying a plurality of vertically disposed imperferateribs or dams integral at least with the underside of the perforated plate, theplanes of the dams being dis:

posed at right angles to the axis of the corrugations; The

ribs or dams may also extend above the plate, although this is not essential except possibly incertain liquid phase operations. A similar efiect can also be obtained with a design consistingof a plurality of adjacent pyramids or cones, Whose bases are all in the same horizontal plane, made of perforated plate or at least with openings near the top for the light phase'and along the bottom for the dense phase. This baflle would trap the rising gases Without the use of the vertical ribs or dams and redistribute the same or prevent channeling or large bubble formation. This design is more difficult to construct particularly in establishing the necessary ratio of the size and number of the openings at the upper part of the other freearea in the valleys, for usein vesselswith a high net rate ofsolids flow from the bottom to thetop of the unit, where no advantage may exist forpermitting downilow of solids. u

A further possible design consists of a flat horizontal perforated vplate, on top of a gridworkof vertical imfperforate ribs or dams formed like an eggcrate or honeycomb, to provide numerous cells or pockets beneathxthefbafile, fort-rapping; the, rising ,gasiform ma- Patented July is, seen i-f 'lhe' :gridvvork also extend above the the outermost rib member'and the supporting 2 nee d F iQ t -721 4 s e seed-- tribution of liquid flowing downy f h b In the accompanying drawing fth'ere is set forth in a a 2 4 mm) I perforated plate," although this is not essential, except "The corrugated baflle i'nen bers 23 are" preferably "s- 1 that in certain liquid flow cases such dams might be 'cure'd along each edge as by welding to the contiguous dis; rib memberor supporting'ring. It. will berunderstood r 6 ithat'the-bafie structure 'canEbe-ibuiltLup in'place'inare: a Y

actor yesselinwhich evcntthe sl pporting g -niay,*if

Figure-l theessentials of a modern hydro desired, be eliminated." Itzis essential that"? plane ,of f forming plant'equipp ed with bafllesin accordance vvith the p [the riblmembjers tbe'disposed' at-gright angles-ate thesaxis present invention. 1 a i 1;; V of theicorrug'ations and it isadesirablerthatrthe a a Figure} presents anis'o yievy oi the bottom ar a 10 =bers extend some distan fi 'below the corrugated afllef;

' preferred form of the nevvjand improved means of bafg members, for example about S oor 4 'inches. and prfer- 7' fling forming apart of the present invention;; 7 a ably about 8 inch'es or there, depending upon the size I fications olfbafliing means "forming this'inven;

fFigUX'S 3fiand'4 illustrate;in 'ispmetric rievl s tvvo rhodi 3 of the unit and ithe distance-atogthe'levelL .of the dense bed. The rib members should preferably be deep tion. 1 q f n 7 V V 7 M 7 5 enough to contact the' uppersurfaceaof'the densejb'ed. e g n de i IQ Figure 1, figure'r'epresents If desired vertical, imperforateiin'enl'bers.inlay'be ear? 7 V afhydroforming; reactor containing a vfluidized bed' of' ranged b'e'tween the rihmembers and'preferably beneath '7 r a catalyst C disposed within the reactor as shown disposed th'e'vall'eys offth'e' corrugated baflieimmbers to preventpr v 1 on '-a gas;d is tributing;means or -grid iGgfand having an hinderlateral flow or 'rnovement' dffthe gasesgor. vapors upper-tdensephase level-L. 'Theireactor contains two betw een 'the'rib'members. -;The vertically disposed haffles F disposedas'shown'within the said reactor, said perforate ribs"or dams trapth e upilowingtgasiform' ma: 1 fbaflies being illustrated in greatergdetail in Figurel de terialand-1festrict it in horizontal mofidn'iioiihe' Idise; scribedbelow; Naphtha is ,fed to the system through h nef :itances indicated in the drawinggithus forcing'the said 7 g? V z gp ss n lh i i i ling via blinelintb thebeq qf catalyst Q in reactor 1.. Si- 25 of the bafilfiwhichisfirst enterfi d. The gas-solids con foreedjhrougha furnace,6,- ;then withdrawn from said 'to'w ards'theinner wall of the reactorgagglomeratingtwith iurnace throughjline- 7 andehar ged to: the bottom of gas, inother areas 'of :the gvessekand thenifchanneling f; taining .gas flow upwardlythrqugh'thebed ofcatalystat large gas bubbles The gases.flow'primau-ily:upthrough fter throu gha furnace?! and thencepas gasiform materialup through lthe' peakinztha't section 'multanep'usly hydrogen-containing gas, usually obtained tactingefiiciency is'greatly improved, bec'auseithe'gash from theproductreeovery'systemand flowing in line 5, is form material is thus prevented "from'flowingdateraHy reactor 1. The heated pil vapors and hydrogen con V upwardly in the form of either a cdntinuous "streamer;

a relatively glow superlicial velocity; say 0.2 2.0 feet the baflie 'p'eaks andthe scli ds-gflow Idown; throughithe' fig, QWDQLfiQQMflYS? W ichiis in thel-formof-apo dgr Valleys resulting inj very-'uniform' distribution;ofghothl I 7 by the gasiform rnateriaL; ,For'bestfluidization the cataforations in thebhfiie, means pfropreri which :arePo'f the I lygz shoul d contain 1 1151 1 m, percent, p f bl ."ordei' of Tone-half toithree inches :in diameter, ;arefcloselymeans in'accordance withgthe present inyentiongexcellent V to40 micron particles, s'paced, so. thatthe free area of; thebafde -is from: about although because} of; great efiectiveness of; the bafflin 3- '10 to %;fpre ferably 20 t040%j1 b f,iheltqtaifcibssr sectional area of the reactor; Thepressureidropithrough- V: ontac Qfl Q 'JY isflealized fi lr gh the, catalyst 40 ;the -bail1e' means fpreferably does not exceed'l 0,5 p.s'.i. i V Q V J S Q 1 1 Wt- 'percen't ofjMfl micronf partb 'so'that sonie solids cani flow down throughzthe v V 1 jcl'es. [Underthe proper conditions oftemperature-pres which: cause the formation of a'mmimum dilutecoridlsg r .lsure'and a suitablecatalyst,gthe,desired hydroforming p'e'rs'e phase ofcatalystand gasiform' material below-tithe jQintoa ygas, separation space positioned between L and C1 1? and the raw vapors pass-from the'bed of catalyst baflles thus permitting substantially "complete'wutiliza 45 tion'of the volume of the reactor space.

the top of the reactor wherein the mainv bull: of the S Pointed fthat the perforations inthe baflle .catalyst is separated from the stream and descends toward p s a P effiffed m d t n, 633?- V a i thg' bed B, ,Befgre the vapors are withdrawn 'the that 1116 perforations may be Of thB OI'deIFOf 0116311111 reactor; they are forced through one or more cyclones -S wherein catalyst still entrained in the vapors; is sepa- 9, thence conveyed by line 10 to a separator ll "wherein 55 Y be at an l abmjlt 0 1 9 12 55 's'with 'the' gasiform material is separated from the liquid material horlmtal Qorrespsndmg'to corrugation 211181505 from and recycled via line 12 to line 5 for further use in about to about The'bames y be constructed rejected from the system through line 13. The liquid 1 Arnmrnb'er of factors are involved in determiningihe from which product is recovered through line 16 and B any i amaldistribuflon'of p q 'i "delivered to storage 17. Light tnaterial is Withdrawn g g w gii mi g gf z SameUPiieFnIt 59 I overhead from'lslthrou hlin 18' d tili a a Y appr cpowervorssi'an g e an H zgd m known ids attrition, and permit sufficient solids downflowetoimj f,=

"manner; Exceptsfor the baflles F disposed in reactor l, V the process indicated immediately"above'represents the a essentials'of'a commercial hydroformin'gplant In Figure 2 there is a represent'ation of a preferred} 50 'onehalf inches: in diameterand spaced apart threeand three-eighth inches from the center to' center and that the rated and returned'to the bed by one or more dip heightof thepeaks-from the bas elofthedepressionsior pipes d. .The vapors are'withdr'awn. from the reactor Valleys b 9 the wider 0f about Six totwelveimhes via line,8, cooled to a temperature of about 100% F. in V furthermore the Planes formed bythe fi the process. Excess hydrogen-containing gas .may be fmmPeI'fOTiitB Steel having a'thickfless 0f I product is withdrawn from the separator 11 through line 60 Ptim11mPrSSPIe drop (and? hence free afeayfor W 14 and charged to a fractional distillation 'column 15 bafie" The Prgssure drop Should be ihlgh enough'to employing the fluidized solids technique; ,t a -Figures: 3fand 4 illustrate'lnodifi'e dforms oftbaflles,

'form of theiniproved bafiles. In' the'modific ation there Z whi arera'pable' off-giving resultsithatare, comp'ammc a l a show/11,; the baffles comprise several Verticalimperforate, -rib members ,21 arranged parallel'to each other and se;

curedat 'theirends' to a supporting ring 22. A perforatwith vthose achieyed 'with the .bafliel arrangement 'ofiiEig' "l e 2.. The baflieshown inj'Figi reia comprisesla 'multil icityJof verticaI,"taperedwmembersi31=1i1r1thei=fornr1of v -hollow cones orfpyramids havingbpeningsi 32: at'ornear" i ed undulating 'or corrugated baflle 'memberl23 .is arranged between'each of the rib'member 21 and betw'een nxtheir apeXes fOI'QZtheQdiSChKIgc;pfllipflov ing gas or a.

Ling uniform distribution of the gas or vapor or the cellular structure beneath the grid;

apt-gees pa fena'materin alone "or admixture with ma (1ied solid contact or catalyst particles and additional dpenihg's33 at or near their bases forthe discharge or recirculation of solid contact or catalyst particles to the space below the baflie or gas redistributionmean's. The size and the number of holes for the members 31 may 'be'the same or difierent at the edges as compared with through the said cone and ent- -at thtciP'therof'firid ther'eb'y preventing the ae'enrnulaaen nd (discharge-of -a major portion'df the gaseous er va'porou'smaterial through a small or limited area of the bane.

The baflie of Figure 4 comprises a plurality of livertical, imperforate sheets or strips "of metal 41 and f 42 "secured at least at their ends to the inner wall 'of the vessel 'or to a 'mounting'ring or the like for attachment to the interior of the vessel. The sheets or ribs 41 and "42 are arranged at a suitable angle to each other, de-

sirably at a 90 angle in order to form'an egg-crate or "cellular structure'which limits lateral or cross flow of gaseous or vaporous materials during their passage there- "throu gh. A perforated plate or grid 43 is secured to the top df the sheets or ribs '41 and 42 in order to redis- "pers e thegas'eous or vaporou's materials as they are dischanged from each of the cells'formed by the sheets or fibs 41 'ahd 42. Similarly to the perforated she'ets'of 't-he bathe illustrated in Fi'gur'e '2, the size and distributi'on 'ofthe'holes in grid 43 is such thata low pressure drop, 'i.e. less than about'0.5 p.s.i. is taken in passing through the bathe assembly. This form of baflie is very simple tdcb'nstruct and yet is highly efiec'tive in achievflow because I A S-foot diameter high pressure fluidization unit having a height of 40 feet was utilized to study contacting efiiciencyof gases with finely divided solids. The solids used in the study were a hydroforming catalyst consisting bf'about l wt. percents/1e0 88 wt. percent Al o and percent SiO Th'e'unit was pressurized to 80 "psiag. and'the' catalyst particles were fluidized with air at 0.8 ft'. per second superficial velocity, conditions which simulate closely the fluidiz'ation in commercial fluid hy- Hififormers. Using helium tracer methods, the contactiiig efficicncy was determined and 'compar'ed with the cdntacting, eff ciency that was determined for the particular hydroforming catalyst in a inch diameter, 40-foot iiluidhydroforming pilot plant. Studies were made with a coarse catalyst mixture containing only 4 wt. percent of micron particles, with a second mixture containing 78 wt. percent of 0-40 micron particles and a third mixture containing about 10-11 wt. percent of 0-40 micron particles in the unbaflied vessel and in the 'unit when provided with corrugated, perforated baffles 'asjishown in Fig. 2 in which the vertical plates or dams spaced about one foot apart to which strips of plate with evenly spaced holes in diameter (32% free area) folded into corrugations 6" deep were welded along their edges. The data are summarized in Table I.

to improve contacting efficiency in fluid beds.

These datash'ow that the cerrngatedbaflies inlae- "cordance with the present invention etfecfia substantial improvement in contacting efficiency upon a weight-basis as well as upon a volumetric basis with catalyst compositions deficient in fines (4% 0-40 micron material) --as 'well as with compositions containing suflicient fines to permitw'good fluidization. The baflles-were most elfective improving the contacting einciency with the catalyst -ciintain'ing only 4 wt. percent of 040 micron particles. The?advahtage"of'lowpressure bafiies in fluidised beds lies in'the 'fact' that they permitia reasonahleamount of dumping or catalyst movement through the baffles. This -helps to decrease disperse phase formationand prevent "catalyst segregation. also harmful since this will permit emulsion.gasback- However, too "much dumping is mixing. Experimental studies involving radioactive solids mixing tests'in the high pressure fluidization unit ofE-x- 'ampl'e l haveshown that the 'd'umpinfg rate is a .functionof (1) free area and (2) fines concentration. in.-

creasing both tends to increase catalyst dumping. in

-general, the lower the fines (040 micron) concentration the greater the free area of the baffle may be.

The reason for this is'that there is a zone of low co'ncen'tration below each baflie. "As a result, it has been determined that there is an optimum number of baffles to be used; with more'thant'he optimum number the "decreased catalyst inventory more than counter-balances the small further improvement inefficiency. Specificalabed depth'of momma, it is most advantageousto utilize two spaced cellularized bafliles in accordance with number of embodiments of the present invention. It will be'understood that this invention is notlimite'cl thereto since numerous variations are possible without departing from the scope of the claims herein.

What is claimed is: v

1. A method for improving the inter-phase contacting ina multi-phase fluidized solids process which ce'rn'prises causing a lighter gasiform phase to flow upwardly through adense phase comprising particulate fluidizable solids, subdividing the upwardly flowing lighter gasiforin phase passing through a lower portion of the dense phase into a plurality of'small confined and separated streams and baffling lateral flow of said streams, then'further subdividing each of said confined streams-into a multiplicity of smaller streams which are discharged into and intimately dispersed in the dense phase immediately there- 'above.

2. A method for improving gas-solids contact in a fluidized bed of solids which comprises charging'finelydivided solids'to a reaction zone, introducing a ga'siform material at the bottom of said reaction zone at a velocity sufiicient to maintain said finely'divided solids as a dense.

fluidized bed, subdividing the upwardly flowing gasiform material passing through a lower portion of the dense fluidized bed into 'a pluralityof smallconfined streams and preventing lateral flow of said streams, then further subdividing each of said confined streams into a multiplicity of smaller streams'which are discharged ifito and; intimately-dispersed in the dense fluidizedwbedimmedh sufiicientto maintain said finely divided solidsiastardense,

-fiuidized' bed, subdividing the .upwardly'flowinggasiform 'inaterial'passing'through a lower portion of thet'dense fluidizedbed'into a plurality of small confined streams j, ,gasiform-nraterial from theft'opofrsaidi vessel, redistributang means arranged at at least-one intermediate level of a said vessel comprising aplurality. of vertical; 'imperiorate material into a number of streams prevented from, flowing laterally before said istreams are subdividedfing fiow- 'ing through .perforationsf of the corrugated 'metal' grid members. V

- terials and finely divided solids-and for the downward 'passage' of finely divided solids and entrained gasiform- "material'fcellula'f means provided on'the under 'side of g said' re'distributing means for trapping the rising gas and'preventin'g lateral flow of said streams, then further it! 8. A reactor 'vessel, means for supplying gasiform masubdividing each of said confined streams into a multiterial at the bottom of saidvesselQmeans for remoying plicity--qf smaller streams which are discharged into/and .gasiform material from the topof'saidvessel, redistributintimately dispersedin the dense fluidized bed immediateingtmeans arranged at at; least one intermediate level Qf lythereabove and discharging a limited amount of; the said vessel comprising aplurality of verticahimperforate' solids in the last namedrfluid bedtdownwardly-into'aeach '10 rib members arranged in spaced relation across said of said smallconfined streams of rupwardly flowing' gasivessel'dividingthat'portionof the'reactor intoa plurality 7 form material I i z: :1; oi'vertical' passageways to subdivide-gasiform material. V :--4. An improved method forrhydroforming hydrqcar't- "flowing upwardly therethrough into 1 small confined bon fractionsboiling: within -the;motor fuel-or naphtha "streams, andiperforatedcorrugated metal members boiling range which comprises charging 'a reaction zone It! with a multiplicity of perforations arranged betweensaid a with ,finely idivided hydroforming catalyst, introducing b members wi h a of h w a Q tr h naphtha vapors and hydrogen-containing gastheretorat'a angles to the plane of said rib members to furthe r;sub-

, superficial velocity of from'about 0.4 toabout 2.0 per dividesaid confined streams into aniultiplicity of smaller a second suflicient' to maintain, the catalyst as: atdense, streams, said rib members extending several inchesbelow e fluidized bed, maintaining V the reaction zone i at antern- 20 the bottom of the valleys of said corrugated grid members;

perature between about 850'andi1000" F. and at presr 9. Theapparatus as defin in claim 3 1- h sures of up to about 500 .s.i.'g., Lsubdividin'gthe upp rfor t d grid mem r h v a r a e f about 1 wardly flowing vaporousand gaseous materials passing 50% Of thevessel CfOSS on- V 7 J through a lower portion ,of'ther dense fluidized bed of a aC r vessel, means for pp y n a m as finely divided hydroforming' catalyst into a plurality of t rial a t bottom of i vessel, means r' mo ins small, confined streams and preventing lateral flow; of ,gasiform material from the top of said vessel, redistributsaid streams; then further subdividing each of said icon ling means arranged at at least one intermediate level r fined streams 'into;a:;r nultip1icity of's'maller streams which vWithin Said Vessel pr in i 'p u o dv r ,are discharged into'and'intimately dispersed 'in the dense, p fi Wall members D I 5- T r atrqi' f fluidized bed of catalyst immediately thereabove. *t o divide that portion of the vessels into ajpluralityg'of ts, Animproved method for hydroforming hydrocarbon r l i ely. small vertical pp wav ce ls f o r hisz ft-actions boiling within ,themotorfuel or naphtha boiling lateral O gas flowing P fll h aQ I lL P QE Irange whichrcomprises charging a reaction zon ith vented by said wall, members, ailld fa, perforatedfgrid' ,finely divided hydroforming catalyst,-introducing naphtha member having a multiplicity of P If l' Q I Qt'i 3 Y ,vapors and hydrogen-containing gasthereto at-a super- 3 h p5 ofsaid rimpeffolfatr 311: mb s 'Qfifi-at V :ficial velocity of from about 0.4 to ab utzo fl per redistribution of the gases discharged from said cellsias second sufiicientl'to maintain the catalyst-as a dense, Smaller Stream? than. stream pa u 39 fluidized bed, maintaining the reaction-zone at atem-i said Cens- 1 1 f 1t ,perature between about 850 and 1000": and at pres- The apparatus 5: defifiedill fl il l n w i ith sures 0t up toabout 500 p. s.i.g., ;subdividing the upward- 49 "Perforated grid 1116111136? 3 re 2 about 02 11y flowing vaporous and gaseousfmaterials passing'through 9 of thevessel SS 5 I a p:

a lower portion of the dense fluidized bed o'fifinely divided a a s l an i r Su yi i mr I thydroforming catalyst into a'plurality of small, confined 'i t the bottom a V s f lr mqvm streams and preventing lateral flow of said streams, then gasifol'm material m i top il Said s i 't d t l' bl i' Y further subdividing each {of said confined streams into, a 4 5 2 means arranged leastjdile intermediate level i 'multiplicity of smaller streams which are discharged i ,in said vessel comprising a pluralityrof essentially cone; andintimat'ely .dispersed inj the dense; fluidized-bed of .shapsdrredistribufing ekmenm a n d w h nthws is 1 catalyst immediatelythereabove and discharging a li i d ,with their bases essentially one horizontal p1ane,per-Z;

, amount Dime catalyst in the, last named fluidized bed forations in the upper po of a d s sp d id intoeach of said small confined streams 'of upwardly 71116113 for the discharge of 8 1 5 materials and P ,fiowing vaporous and gaseousjnate -ia1 forations at the lower portion of ,said cone-shaped ele 6. A reactor vessel, mean f supplying if ments for the discharge of finely divided solids thereterial'at the bottom of said vessel, means for removing through, each p element forming a pas gasiform material from the top of said vessel, redistributwhich an upflowing Stream of gasifol'm material is ;ing means arranged atat least one intermediate level withfined and pl'evenffid from moving lateially to l j n in said vessel comprising a plurality of imperforatewall ewe-shaped element a memb arranged to bdi i the cross Sectional area 7 13. A reactor vessel for the contacting of gasiformmaof the reactor into a plurality of relatively small, verterials with a dense fluidized bedpf finely i Solid 7 tical passageways each of which confines an upward Particles wmrrisiflg a Vertical vessel, means for supply" 7 .fiowing stream therein to prevent lateral flow and permg gasifol'm materials to the 'PQ iQ Ofls'ajd forated bafiie means gath f of said p s vessel and means for removing gasiformlmateria'l from w; ways witha number of perforationsto subdivide the thus 111.6 upper P l of a e f i ufin m r V a m g d fam 'from'each of said'passageways. arranged at 153st one intermediate leveliwithil'lf'ihg i 7 A a vessel; mcans fo u lyi if m dense fluidized bed comprising a bafllemember-provided :Wfii 1 1 bottom of said vessel, means .for removing openings'ifor upward'passage o o i m rs: arranged in; spacedirelationi afcross said ,7 2....vssss i iridin hatgp flon q t egrea -int ;a n uraiity V, j {of vertical'passageways,and perforated;corrugatedimetal I i a grid membersmr anged between said. ribfrnembersgwith streamsfandjminimizing the: lateralfiow thereofikthereby I achievingmoreUniformdietribirtibhof the gasiform'mm '2 terial in the zone abovethesaid redistributing means 1 1' I;the,axis'tof thetcorrugations at right angles to theplane Prevafled in bed m a e r vwi aidr d st il i 1 of'saidrili nieinbefsfsaid rib members and said corrumg w- I i it" i i l.8 ml, lf dl sl fi g l d fi b m. U 1 ;(Refere nc,esjonifollowinglpagel-i 9 References Cited in the file of this patent 2,740,752 UNITED STATES PATENTS 2,472,502 Tyson June 7, 1949 2,581,134 Odell Jan. 1, 1952 2,606,104 Hogan et a1. 2 Aug. 5, 1952 120,335

19 Auburn Apr. 3, 1956 Dineen et a1 Ian. 15, 1957 Hemminger Dec. 17, 1957 FOREIGN PATENTS Australia Sept. 13, 1945 

1. A METHOD FOR IMPROVING THE INTER-PHASE CONTACTING IN A MULTI-PHASE FLUIDIZED SOLIDS PROCESS WHICH COMPRISES CAUSING A LIGHTER GASIFORM PHASE TO FLOW UPWARDLY THROUGH A DENSE PHASE COMPRISING PARTICULATE FLUIDIZABLE SOLIDS, SUBDIVIDING THE UPWARDLY FLOWING LIGHTER GASIFORM PHASE PASSING THROUGH A LOWER PORTION OF THE DENSE PHASE INTO A PLURALITY OF SMALL CONFINED AND SEPARATED STREAMS AND BAFFLING LATERAL FLOW OF SAID STREAMS, THEN FURTHER SUBDIVIDING EACH OF SAID CONFINED STREAMS INTO A MULTIPLICITY OF SMALLER STREAMS WHICH ARE DISCHARGED INTO AND INTIMATELY DISPERSED IN THE DENSE PHASE IMMEDIATELY THEREABOVE. 